Hydroprocessing of heavy crudes by catalysts in homogeneous phase

ABSTRACT

This disclosure relates to a procedure, which through the application of a catalyst in homogeneous phase, allows the transformation of heavy hydrocarbons (vacuum residue, atmospheric residue, heavy and extra-heavy crudes) into hydrocarbons of lower molecular weight, characterized because after its application, the hydrocarbons obtain greater API gravity, lower kinematic viscosity and different composition by hydrocarbon families (SARA) that increases the proportion of saturated and aromatic resins and asphalts. The sulphur and nitrogen content is also reduced, resulting in higher yields to high commercial value distillates and a lighter product as compared to the original crude.

CROSS-REFERENCE TO RELATED APPLICATIONS

This patent application is a divisional of U.S. Patent Application No. 16/932,326, filed Jul. 17, 2020, which in turn claims priority to Mexican Patent Application No MX/a/2019/008622, filed Jul. 19, 2019, the entire disclosure of which is hereby incorporated by reference herein.

TECHNICAL FIELD

This disclosure relates to the field of technologies for the improvement of petroleum crude oils, through changes in their physical and chemical properties, for example: increased gravity API, decrease in viscosity, increase in the proportion of saturated and aromatic, the increase of distilled fractions (gasoline, diesel and heavy gasoil) and decrease in the amount of long-chain paraffin resins, as well as asphaltenes, sulfur, nitrogen, etc.

BACKGROUND OF INVENTION

The oil industry requires the development of more efficient secondary recovery processes and improvement methods, by using alternative methods of exploitation to increase the relative production factor of reservoirs. In addition, the handling and transport of heavy crude oils to refining facilities are relevant aspects for the production of fuels. The heavy oil reservoirs are difficult to exploit due to high flow resistance (high viscosity) and these fluids present a lesser yield of distillates (<538° C.).

Some technologies focused on improving the quality of heavy and extra-heavy crude oils within the reservoir, with the purpose of increasing the recovery factor, i.e., vapor injection in situ (ISSI), simulated cyclic injection of vapor (CSS), Aquatermolysis (AT), Steam Assisted Gravity Drainage (SAGD), In Situ Combustion (ISC) by air injection, and In Situ Combustion through intelligent wells (THAI: Toe-to-Heel-Air-Injection), and other recovery methods in situ that involve the use of heterogeneous catalysts (CAPRI: Catalytic Upgrading Process In Situ) and their combinations like THAI-CAPRI.

Conventional crude oils ranging between 20 to 32°API are extracted from the reservoir primarily by natural fluency aided by artificial production systems, but secondary recovery methods may lead to further recovery. However, heavy crude oils that have densities between 10 and 15° API present particular problems for its extraction by conventional techniques, which makes it that alternative extraction schemes are applied to significantly increase production and recovery factors with the required quality.

Current enhanced oil recovery technologies have limitations for extracting heavy oils, i.e., Steam Assisted Gravity Drainage and Cyclic Steam Injection can be applied only at medium depths around 1,000 m. In turn the air injection technologies present a high risk because the use of air injection that provokes the ignition and propagation of a combustion front from the injector to the producer wells, respectively, with some potential difficulties along the way, i.e., explosion risk, deviation of the combustion front, or flame extinction could occur before making contact with hydrocarbons.

Other methods like THAI (Toe-to-Heel-Air-Injection)/CAPRI(Catalytic upgrading-Process-In Situ) technologies use a vertical injection well combined with a horizontal production well, and use feeding air that is pumped down through a vertical well. When air is pumped, the combustion chamber grows and high temperatures develop inside the reservoir. This heat influx reduces the viscosity of heavy crude oil and causes it to flow further within the horizontal production well. The gas produced from combustion brings the crude to the surface.

The THAI process combines a special vertical and horizontal well configuration with on-site combustion. CAPRI is simply THAI plus a catalyst that is added to around the production well. The idea behind the THAI/CAPRI process is to initiate an underground flame and this causes bitumen or heavy crude flow, at the same time, to improve some properties of crude oil in situ.

In contrast to the above technologies, the present disclosure refers to a procedure for the improvement of heavy and extra-heavy crude oils by applying homogeneous phase catalysts with hydrocarbon and the procedures used during its application, so that the physical and chemical properties of the hydrocarbon are improved, as the API seriousness is increased, decreasing its kinematic viscosity, with a change in composition by hydrocarbon families (SARA), decreasing their sulphur and nitrogen content. Simulated distillation indicates the presence of distillates of higher commercial value, (petrol and diesel) with a lower average molecular weight.

Other crude oil enhancement technologies are contained in the following patents:

Patent application WO2005005581A1 refers to a process for the catalytic hydrotreating of heavy hydrocarbons with high in metals content and asphaltenes, which operates at low pressure, in combination with a type of reactor and feed loading, which together limit the formation of sediments and sludge in the product, thus obtaining a hydrocarbon with improved properties, with a low level of contaminants, higher gravity API and distillates, which falls within the intervals commonly reported in typical feed loads for refining schemes.

Patent application WO2014068390A1 concerns nanoparticulate surfactant formulations that improve the transport of heavy hydrocarbons. The formulation comprises a nanoparticulate surfactant selected from a group consisting of hydrophilic silica nanoparticles, with metallic character or mixtures thereof, plus an ion liquid (IL), non-ionic or non-ionic liquid surfactant.

Patent application WO2009011559A1 reports an ion liquid catalyst for the improvement of heavy and extra-heavy crudes through hydrocracking type reactions and hydrogenation of asphaltenes and resins, which are promoted by Mo and Fe-based ion liquid catalysts. These catalysts are highly miscible in the homogeneous phase within crude oil.

Patent application US20100010282A1 refers to a new procedure either to increase or reduce the viscosity of light or heavy hydrocarbons, respectively, by means of dopamine mixtures, a compound that is combined with other substances, to modify flow properties and increase the electrical load of mixtures and solutions as well as the dissolution of insoluble compounds in water or in aqueous solvents. Some mixtures are designed to modify the proton mobility, thus, the invention showed banana plant juice that contains dopamine and other compounds such as quinones, carotenes and terpenes are responsible for the observed effects, especially for electrical properties and dissolution of metals and its metallic compounds.

Patent U.S. Pat. No. 8,257,579B2 reports a process for dewatering and removing asphaltenes from heavy and extra-heavy crude oils online. The process is applied at the well mouth with pressures of 414 to 689 KPa and at a temperatures range between 60 and 100° C., which includes two stages, one dewatering and one of embezzlement. In the first case the addition of solvent is performed, thus free water is removed, plus heating, use of emulsion-breaking additives and settling for water removal form emulsion. In the second stage the asphaltenes are extracted, which comprise the use of low-effort in-line contactors or mixers, a specific design and use of a sedimentator that contains specific internal components for phase separation. The recovered solvent is recirculated to the process, while the separation of crude oil improves, and asphaltenes are re-arranged as fuels for electric cogeneration, which self-supplies energy requirements for the production and improvement process.

Patent document WO2018/064990 relates a formulation and process of preparation of catalytic materials for hydrocracking processes (HCK) of heavy crude fractions in dispersed bed reactors, from deactivated catalysts in fixed bed hydrotreatment units (HDTs). For preparation, catalyst precursors must undergo a process comprising the following unit operations consecutively: liquid-liquid extraction washing, grinding, drying, calcining and activation by means of elemental sulphur treatment. The present invention is also related to a hydrocracking process in dispersed bed that improves the performance of prepared catalysts.

Patent document U.S. Pat. No. 7,001,504 refers to the use of ion liquids for the partial conversion of sulfur compounds to sulfoxides or sulfones to increase their solubility in the ion liquid and not as in the present disclosure, using an ion catalyst in the presence of hydrogen, to promote reactions of disintegration and hydrogenation.

Patent document U.S. Pat. No. 6,969,693 refers to the use of immobilized ionic liquids in a support as a catalyst in Friedel-Crafts reactions, especially in alkylation reactions, in contrast to the highly dispersed ion liquid catalyst for use in hydro-disintegration and hydrogenation reactions such as the present disclosure.

Patent document U.S. Pat. No. 5,731,101 refers to the use of ionic liquids from metal halide salts and hydro halogen alkyl amines for the production of linear alkylbenzene, in contrast to the iron-based ion liquid catalyst of the present disclosure, which is useful for promoting hydrogenation reactions and hydrocracking of heavy hydrocarbon fractions in heavy crude oil for the production of improved crude oils.

Patent document U.S. Pat. No. 6,139,723 refers to the use of Fe-based ion liquids for application in bitumen and residue.

Patent document U.S. Pat. No. 4,136,013 refers to a catalyst in the form of homogenized suspension of Faith, Ti, Ni and V for the reaction of hydrogenation of crude oil and residues, in contrast to the homogeneous phase catalysts developed in the present disclosure.

Patent document U.S. Pat. No. 4,486,293 uses a Fe catalyst in combination with a group VI or group VIII metal from organic salts of these metals for use in coke liquefaction from a hydrogen donor and a saline aqueous solution. The catalyst is first impregnated in coke before the liquefaction reaction, not with the ion liquid catalyst prepared from inorganic iron and molybdenum salts, which are dispersed into crude oil and not impregnated.

Patent document U.S. Pat. No. 5,168,088 refers to the use of a slurry-type catalyst for coke liquefaction by precipitation of iron oxide in the coke matrix, rather than from an ion liquid catalyst prepared from inorganic iron and molybdenum salts that are dispersed in crude oil and do not precipitate.

The above technologies were widely exceeded, since the catalyst that is object of the present disclosure is of a bi-functional character, presenting an acidic function, which promotes disintegration reactions, while the metallic function promotes the hydrogenation reaction. Likewise, the homogeneous catalyst is anchored to the rock formation of the reservoir, does not require prior activoation and can be used in the oil industry to improve the properties of heavy and extra-heavy crude oils in situ. The severity API is improved from 5-8 units; viscosity is considerably denser, above 99%; the reaction temperature for the treatment of heavy hydrocarbons is 300-490° C. in a time of 0.5 to 4 hours; higher yields to distillates (40-60%) and a lighter product compared to the original crude, also, carbon formation is less than 1% weight.

BRIEF DESCRIPTION OF THE FIGURES OF INVENTION

FIG. 1 illustrates, through a block diagram, the experimental system with rock core.

DESCRIPTION DETAILED OF THE INVENTION

The present disclosure relates to the synthesis and application of a homogeneous phase catalyst, which allows the transformation of heavy and extra-heavy crude oils into lighter oils, by hydro-disintegration and hydrogenation reactions, in a cyclic process either in a reactor belonging to a surface installation or at the bottom of the well, simulating reservoir conditions.

The preparation of the catalyst is carried out in aqueous phase (based on running water, congenital water, and/or brine), using inorganic salts of a metal of groups VIIIB, VIB, IB, such as Fe, Co, Ni, Cu, Mo, W. The preparation of the catalyst of the present disclosure includes the following steps:

-   -   1. Using conventional vessel, phosphoric acid (H3PO4, technical         grade) and ammonium molybding ((NH4) 6Mo7O24.4H2O, technical         grade) are mixed, stirring moderately at 25° C., until a dear         solution is obtained, The pH of the solution varies between 1         and 2.     -   2. In the second step, the nickel sulfate hexahydrate         (NiSO4.6H2O technical grade) is incorporated and solubilized at         40-100° C., preferably 60-90° C., dissolving in running water,         keeping the agitation constant for three hours at 25° C.     -   3. The solution formed above is stored in a closed container         under environmental conditions, where the catalytic solution         must be green and translucent.     -   4. Finally, the catalyst is dehydrated at 90° C., depending on         the type of application to which it will be directed (liquid         phase, gel or particles of the corresponding salts). The final         molar ratio is 1.0 nickel: 0.084 molybdenum: 0.295 H+: 14.42 H2O         at pH 1-3.

The catalyst of the present disclosure, presents high catalytic activity for hydrocracking reactions and hydrogenation of heavy hydrocarbons. The procedures used during its application allow the physical and chemical properties of the hydrocarbon to be improved, decreasing its kinematic viscosity, which allows its fluidization in pipes. It increases the gravity API, changing the composition by hydrocarbon families, (SARA), increasing the proportion of saturated and aromatic, while decreasing fractions of resins and asphalts. Likewise, the sulphur and nitrogen content is reduced, resulting in higher yields to distillates of high commercial value, e.g. gasoline, diesel and diesel, mainly reaction products are not carbon-formed and therefore the liquid yield is very high, greater than 95%.

The evaluations were carried out according to the scheme in FIG. 1 under operating conditions that prevent the generation of coal, optimizing the performance of liquid products. To do this the operation interval is as follows, shown in Table 1:

TABLE 1 Operating Conditions Presssure Kg/cm²  70-120 Temperature: 340-420° C. Reaction time:  0.5-4 h Catalyst Concentration:  0.5 10% w

Results are observed indicating a possible breakdown of asphalt molecules and resins, as well as the removal of sulfur and nitrogen compounds, with an increase in API gravity and a significant decrease in their viscosity.

In order to show unsamped catalyst reference parameters, the conversion of heavy crude oil with a prototype liquid catalyst formulated based on nickel was evaluated. The results are shown in Examples 1 to 4.

The load used for the realization of the different experiments, was a heavy crude of the Golden Strip (North of Veracruz, Mexico), its properties are detailed in Table 2. It was also experimented with rocks representative of a carbonated deposit consisting of dolomites (CaCO3—MgCO3), limestone (CaCO3), magnesites (MgCO3), diatom ites (SiO2—H2O) and mixtures thereto; rocks of the site itself and rock of outcrop analogous to the deposit, as well as synthetic rocks of the type Berea (SiO3—Al2O3—MgO—CaO) and limestone Bedford (SiO—MgO—CaO), which are used both in crushed form to different meshes and/or nuclei with different dimensions.

EXAMPLE 1

The homogeneous Ni-based catalyst was prepared by the aqueous impregnation method. In this method, the required amount of ammonium heptamolibdate [(NH4) 6Mo7O24.4H2O], nickel nitrate [Ni (NO3)2.6H2O], and phosphoric acid [H3PO4], in stochiometric proportions at room temperature and at pH between 2 and 3, with constant agitation, is dissolved.

In a batch reactor with a capacity of 500 mL, 200 g of heavy crude oil and 2.5 g of liquid catalyst made from nickel, with mechanical agitation at 800 rpm, were placed. The ambient temperature is increased to 350° C. at a speed of 5° C./min. Hydrogen is then fed, reaching the pressure of 100 Kg/cm2 in the system. Once the above conditions are stabilized, the reaction time was one hour, starting the cooling of the reactor, and recovering the hydrotreated crude.

EXAMPLE 2

In a batch reactor with a capacity of 500 mL, 200 g of heavy crude oil and 2.0 g of liquid catalyst made from nickel, with mechanical agitation at 800 rpm, were placed. The ambient temperature is increased to 380° C. at a speed of 5° C./min. Hydrogen is fed, reaching the pressure of 100 Kg/cm2 in the system, and once the above conditions stabilized, the reaction time was one hour, starting the cooling of the reactor, and recovering the hydrotreated crude.

EXAMPLE 3

Taking advantage of the porous volume of the rock and its ability to store fluids such as crude oil, gas and brine, the raw oil is saturated with hydrogen in the presence of a catalyst that is anchored to the rock, at a concentration of 2.0% weight. A stainless steel cell, a continuous injection pump for high pressure, with automatic control, and a reverse pressure regulator are required. The cylinders containing the oil are used to perform the injection process, at a controlled speed and pressure, until the oil saturation defined for the test conditions is reached. A core (1.5×2.5″) is placed inside a cell, confinement pressure is applied, vacuumed for a period of one hour and the oil containing catalyst is injected, (same as anchoring to the rock formation is slowly added the necessary amount of crude-catalyst until the desired oil saturation is reached. The ambient temperature is increased to 350° C. at a speed of 30° C./min. Hydrogen is fed, reaching the pressure of 100 Kg/cm2 in the system. Once the previous conditions have been stabilized the reaction time was one hour, the cooling of the reactor starts and the hydrotreated crude is recovered.

EXAMPLE 4

Taking advantage of the porous volume of the rock and the storage capacity of fluids such as crude, gas and brine, the saturation of the crude oil containing catalyst is performed first. At this stage a stainless steel cell, a continuous injection pump for high pressure, with automatic control, and a reverse pressure regulator are used. The cylinders containing the oil are used for the injection process, at a controlled and pressure speed, until the oil saturation defined for the test conditions is reached. A core of (1.5×2.5″) of carbonate formed by dolomites (CaCO3—MgCO3), placed inside a cell, then a confinement pressure is applied and vacuumed for a period of one hour and the oil containing the catalyst that is anchored to the rock is injected, slowly adding the necessary amount of that fluid (crude-catalyst), until the desired oil saturation is reached. The ambient temperature is increased to 370° C. at a speed of 30° C./min. Hydrogen is fed, reaching the pressure of 100 Kg/cm2 in the system. Once stabilized the above conditions is left a reaction time of one hour, starting the cooling of the reactor and recovering the hydrotreated crude. Examples 3 and 4 are illustrated in Table 3.

TABLE 2 Load properties and batch reactor products, examples 1 and 2 Properties Heavy Crudes Example 1 Example 2 Temperature, ° C. 350 380 Pressure kg/cm² 100 100 Gravity ° API 10.7 17 18 Viscosity, cSt 15.75° C. 13,490 135.8 125.7  25.0° C. 4,883 90 69  37.5° C. 3979 55.6 40 Sulfur total, ppm 5.3 3.71 3.58 Nitrogen total, ppm 4994 425 411 Carbon, ppm — 0.5 1.0 SARA, % wt Saturated 16 28.9 31.9 Resins 36 12.6 10.9 Aromatics 25 44.7 46.9 Asphaltenes 22 13.7 10.3 SimDis TIE 73 66 62 5.0/10.0 154/219 156/196 172/241  15/20 269/310 223/248 2511277  25/30 347/382 270/290 306/347  35/40 415/445 309/326 387/401  45/50 477/506 345/364 426/452  55/60 530/550 383/403 481/511  65/70 569/591 425/451 536/557  75/80 614/680 487/529 579/604  90/95 691/518 614/655 652/669 TFE 744 731 735 Gasoline: TIE-221; Diesel: 221-343; Heavy diesel: 343-540; Resids: 540+ (TIE: Initial boiling temperature; TFE: Final boiling temperature).

TABLE 3 Loading properties and products in a rock core, examples 3 and 4 Properties Heavy Crude Example 3 Example 4 Temperature, ° C. 350 380 Pressure kg/cm² 100 100 Gravity ° API 12.5 17 18 Viscosity, cSt 15.75 C. 13,490 135.8 125.7  25.0 C. 4,883 90 39  37.5 C. 1,550 55.6 24 Sulfur total, ppm 5.56 3.71 3.2 Nitrogen total, ppm 4494 425 1699 Carbon, ppm 1.0 1.2 SARA, % wt Saturated 16 28.9 30.4 Resins 36 12.6 10.9 Aromatics 25 45.7 37.4 Asphaltenes 26 12.7 9.4 SimDis TIE 73 32.8 78 5.0/10.0 154/219 106.5/115.4 124/151  15/20 269/310 138.2/157.1 165/179  25/30 347/382 171/190 192/205  35/40 415/445 201/216 219/232  45/50 477/506 229/244 245/259  55/60 530/550 259/274 272/286  65/70 569/591 291/309 300/314  75/80 614/680 332/351 330/350  90/95 691/518 415/483 405/457 TFE 744 503 608 Gasoline: TIE-221; Diesel: 221-343; Heavy diesel: 343-540; Waste: 540+ (TIE: Initial boiling temperature; TFE: Final boiling temperature)

EXAMPLE 5

5 g of liquid catalyst formulated with nickel is impregnated in 250 g of ground rock of magnesites (MgCO3) and diatomites (SiO2—H2O) in mesh 40, the stirring is constant for 2 hours to achieve its perfect homogenization, and is left to rest for 4 hours. Subsequently, the crude oil was saturated at 24% (heavy crude). The continuous flow reactor is loaded with 325 g of the mixture of fluid composed of heavy crude oil -ground rock- catalyst, compacting it in the reactor evenly, then pressing the reactor with nitrogen to verify its watertightness, after 30 minutes the nitrogen is replaced by hydrogen at 100 Kg/cm2. Heating starts at a speed of 20° C./min, to reach the temperature from the ambient to 380° C. Once the temperature has reached the reaction after two hours, then the reactor is cooled to the ambient temperature. The amount of crude oil in the separator is quantified to determine the index of conversion and physicochemical properties.

EXAMPLE 6

5 g of a liquid catalyst formulated with nickel in 250 g are impregnated with ground rock of outcrop analogous to the carbonated deposit with mesh 40, then left to rest for 4 hours. Then the saturation of the rock core was performed with crude 24% (heavy crude). This impregnated core is loaded into a continuous flow reactor; 325 g of the mixture of heavy crude-ground rock-catalyst, are compacted in the reactor evenly, the reactor is pressed with nitrogen to verify its tightness, and after 30 min the nitrogen is replaced by hydrogen at 100 Kg/cm². Heating starts at a speed of 20° C./min, to reach the temperature from the environment up to 350° C. Once the temperature is reached, the reaction takes place for two hours, then the reactor cools to room temperature to start recovery. The recovered product is quantified for the amount of crude in the separator to determine the recovery rate and physical and chemical analyses are performed.

TABLE 4 Loading properties and reaction products in the porous medium (ground rock) Properties Crude Example 5 Example 6 Temperature, ° C. — 380 350 Pressure kq/cm2 — 100 100 Gravity ° API 12.5 17 18 Recovery, % — 80 65 SimDis TIE 73 59 70  5.0/10 154/219 180/237 170/222   15/20 269/310 281/317 263/298   25/30 347/382 350/387 329/359   35/40 415/445 414/442 390/419   45/50 477/506 473/500 448/480   55/60 530/550 524/543 507/530 +65/70 569/591 560/578 547/565   75/80 614/680 600/619 586/607   90/95 691/518 665/693 657/686 TFE 744 716 715 Gasoline: TIE-221: Diesel: 221-343: Heavy diesel: 343-540: Waste: 540+ (TIE: Initial boiling temperature: TFE: Final boiling temperature)

EXAMPLE 7

The homogeneous catalyst made from Ni in congenital water, was supported in gamma alumina (ABET s 225 m2/g, Pore volume s 0.40 cm3/g, average pore radius x 3.2 nm, particle size 0.20-0.32 mm). In a batch reactor with a capacity of 500 mL, 200 g of heavy crude and 2.5 g of liquid catalyst were placed, the ambient temperature is increased up to 380° C. at a speed of 5° C./min. Subsequently, hydrogen is fed, reaching the pressure of 100 Kg/cm2 in the system. Once the previous conditions are stabilized, the reaction time was one hour, the cooling of the reactor starts, and the hydrotreated.

XAMPLE 8

The homogeneous catalyst made from Ni in congenital water, was supported in mesoporous material (ABET s 1200 m2/g, Pore volume 0.42 cm3/g, average pore diameter s 2 nm, particle size 0.3 mm). In a batch reactor with a capacity of 500 mL, 200 g of heavy crude and 2.5 g of liquid catalyst were placed, the ambient temperature is increased up to 380° C. at a speed of 5° C./min. Subsequently, hydrogen is fed, reaching the pressure of 100 Kg/cm2 in the system. Once the previous conditions are stabilized, the reaction time was one hour, the cooling of the reactor starts, and the hydrotreated crude is recovered.

TABLE 5 Load properties and catalyst reaction products supported in alumina and mesoporous material Properties Residue Example 7 Example 8 Temperature, ° C. — 380 350 Pressure kq/cm² — 100 100 Gravity API 15.5° C. 4.0 12 10 Viscosity, cSt 322900 270 545 Sulfur total, ppm 5.64 3.26 4.42 Nitrogen total, ppm 760 381 478 SimDis TIE 117 90 97 5.0/10 194/229 190/216 211/224  15/20 269/310 245/320 249/342  25/30 351/387 340/367 363/378  35/40 415/445 387/407 402/420  45/50 477/506 426/446 439/460  55/60 530/550 469/490 481/501  65/70 569/591 511/533 522/542  75/80 619/670 556/571 563/589  90/95 687/698 630/669 641/670 TFE 744 713 715 Gasoline: TIE-221; Diesel: 221-343: Heavy diesel : 343-540: Residue 540+ (TIE: Initial boiling temperature; TFE: Final boiling temperature) 

1. A procedure for the preparation of a catalyst, comprising:
 1. mixing a mineral acid and ammonium salts, and shaking the mixture at a temperature of 25° C. until a clear solution is obtained, with a pH variation between 1 and 2;
 2. incorporating Nickel salts into the clear solution and solubilize at 40-100° C., then dissolving in water, and maintaining agitation of the solution for a time of 3 h at a temperature of 25° C., resulting in a green and translucent solution;
 3. storing the green and translucent solution in a closed container under ambient conditions; and
 4. dehydrating the catalyst at 90° C., wherein the catalyst has a final molar ratio of 1.0 Ni, 0.084 Mo, 0.295 H+, 14.42 H₂O, at pH 1 to 3; and wherein the catalyst transforms heavy and extra-heavy crude oils into lighter oils.
 2. The procedure for the preparation of a catalyst, in accordance with claim 1, wherein during preparation the water can be one of running water, congenital water, or brine.
 3. The procedure for preparation of a catalyst in accordance with claim 1, wherein the catalyst is used in a reaction with heavy crude, feeding hydrogen to raise API gravity and results in lowering the viscosity of the oil, increasing the proportion of saturated and aromatic, and decreasing the amount of long-chain paraffinic resins, asphaltenes, sulfur and nitrogen.
 4. The procedure for preparation of a catalyst in accordance with claim 3, further comprising using the catalyst in loads with API gravity of 1 to 14 and viscosities in the range between 60,000 to 1, 000,000 cSt at 65° C.
 5. The procedure for preparation of a catalyst in accordance with claim 3, further comprising using the catalyst in a liquid phase, gel or dehydrated phase.
 6. The procedure for preparation of a catalyst in accordance with claim 3, further comprising using the catalyst in a supported form.
 7. The procedure for preparation of a catalyst in accordance with claim 6, wherein the supported catalyst presents a specific BET specific area between about 30 and about 1250 m²/g.
 8. The procedure for preparation of a catalyst in accordance with claim 7, wherein a support for the supported catalyst is selected from a group consisting of SiO₂, TiO₂, ZrO₂, Al₂O₃, SBA's and MCM's.
 9. The procedure for preparation of a catalyst in accordance with claim 8, where the reaction temperature is between about 350 and about 410° C., at a pressure up to about 50 to about 140 Kg/cm² and a time of about 0.5 to about 4 h.
 10. The procedure for preparation of a catalyst in accordance with claim 9, wherein the catalyst is anchored to a rock formation.
 11. The procedure for preparation of a catalyst in accordance with claim 10, wherein the rock formation comprises rocks selected from a group consisting of dolomites, limestones, magnesites, diatomites and mixtures thereto, rocks of carbonated deposit, and synthetic rocks of Berea or Bedford limestone.
 12. The procedure for preparation of a catalyst in accordance with claim 11, wherein the catalyst is injected directly into the injector well of a reservoir of the rock formation.
 13. The procedure for preparation of a catalyst in accordance with claim 12, wherein the rock formation further comprises a carbonated deposit at a variable ratio of 1 to 10% weight with respect to hydrocarbon.
 14. The procedure for preparation of a catalyst in accordance with claim 13, further comprising activation of active metals carried out on-site at the rock formation.
 15. The procedure for preparation of a catalyst in accordance with claim 14, further comprising a coke generation of only 0.001-0.6% weight.
 16. The procedure for preparation of a catalyst in accordance with claim 15, wherein use of the catalyst promotes the disintegration of resins and asphaltenes to hydrocarbons of lower molecular weight, said hydrocarbons including heavy gas oil, diesel and gasoline. 